WO2015054554A1 - Culture cellulaire à métabolisme optimisé - Google Patents

Culture cellulaire à métabolisme optimisé Download PDF

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Publication number
WO2015054554A1
WO2015054554A1 PCT/US2014/059993 US2014059993W WO2015054554A1 WO 2015054554 A1 WO2015054554 A1 WO 2015054554A1 US 2014059993 W US2014059993 W US 2014059993W WO 2015054554 A1 WO2015054554 A1 WO 2015054554A1
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cell culture
cells
cell
lactate
culture
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PCT/US2014/059993
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English (en)
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Shawn Lawrence
Ann KIM
Amy Johnson
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Regeneron Pharmaceuticals, Inc.
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Priority to KR1020237008467A priority Critical patent/KR102610425B1/ko
Priority to JP2016547976A priority patent/JP6663854B2/ja
Priority to AU2014331776A priority patent/AU2014331776B2/en
Priority to SG11201601681QA priority patent/SG11201601681QA/en
Priority to PL18161278T priority patent/PL3351620T3/pl
Priority to MX2020011334A priority patent/MX2020011334A/es
Priority to MX2016004564A priority patent/MX2016004564A/es
Priority to EA201690600A priority patent/EA033783B1/ru
Priority to EP14851841.8A priority patent/EP3055409B1/fr
Priority to EP18161278.9A priority patent/EP3351620B1/fr
Priority to US15/028,521 priority patent/US20160244725A1/en
Priority to CA2926049A priority patent/CA2926049C/fr
Priority to DK14851841.8T priority patent/DK3055409T3/en
Priority to CN202210497778.2A priority patent/CN114717196A/zh
Priority to ES14851841.8T priority patent/ES2678945T3/es
Priority to KR1020167009163A priority patent/KR102243980B1/ko
Priority to KR1020217011547A priority patent/KR102358807B1/ko
Priority to CN201480055499.4A priority patent/CN105637085A/zh
Priority to EP20193898.2A priority patent/EP3812453A1/fr
Priority to PL14851841T priority patent/PL3055409T3/pl
Priority to KR1020227003381A priority patent/KR102510238B1/ko
Application filed by Regeneron Pharmaceuticals, Inc. filed Critical Regeneron Pharmaceuticals, Inc.
Publication of WO2015054554A1 publication Critical patent/WO2015054554A1/fr
Priority to ZA2016/01550A priority patent/ZA201601550B/en
Priority to IL244511A priority patent/IL244511A0/en
Priority to US15/130,780 priority patent/US20160244726A1/en
Priority to HK16111206.9A priority patent/HK1223122A1/zh
Priority to IL262833A priority patent/IL262833A/en
Priority to US16/984,531 priority patent/US20210087535A1/en
Priority to AU2021200193A priority patent/AU2021200193B2/en
Priority to US17/843,121 priority patent/US20220315644A1/en

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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N5/00—Undifferentiated human, animal or plant cells, e.g. cell lines; Tissues; Cultivation or maintenance thereof; Culture media therefor
    • C12N5/06—Animal cells or tissues; Human cells or tissues
    • C12N5/0602—Vertebrate cells
    • C12N5/0681—Cells of the genital tract; Non-germinal cells from gonads
    • C12N5/0682—Cells of the female genital tract, e.g. endometrium; Non-germinal cells from ovaries, e.g. ovarian follicle cells
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N5/00—Undifferentiated human, animal or plant cells, e.g. cell lines; Tissues; Cultivation or maintenance thereof; Culture media therefor
    • C12N5/06—Animal cells or tissues; Human cells or tissues
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N5/00—Undifferentiated human, animal or plant cells, e.g. cell lines; Tissues; Cultivation or maintenance thereof; Culture media therefor
    • C12N5/10—Cells modified by introduction of foreign genetic material
    • C12N5/12—Fused cells, e.g. hybridomas
    • C12N5/16—Animal cells
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K16/00—Immunoglobulins [IGs], e.g. monoclonal or polyclonal antibodies
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N5/00—Undifferentiated human, animal or plant cells, e.g. cell lines; Tissues; Cultivation or maintenance thereof; Culture media therefor
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P21/00—Preparation of peptides or proteins
    • C12P21/02—Preparation of peptides or proteins having a known sequence of two or more amino acids, e.g. glutathione
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07K—PEPTIDES
    • C07K2317/00—Immunoglobulins specific features
    • C07K2317/10—Immunoglobulins specific features characterized by their source of isolation or production
    • C07K2317/14—Specific host cells or culture conditions, e.g. components, pH or temperature
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N2500/00—Specific components of cell culture medium
    • C12N2500/60—Buffer, e.g. pH regulation, osmotic pressure
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N2511/00—Cells for large scale production

Definitions

  • the present invention relates to cells that metabolically shift to lactate consumption in cell culture.
  • a switch to a lactate consumption metabolic profile in seed train culture has beneficial effects on production culture.
  • cells Upon inoculation of the production reactor, cells exhibit a more efficient lactate metabolism with a low lactate production rate, low peak lactate levels, an early switch to lactate consumption, and subsequently increased productivity in fed-batch mammalian cell culture.
  • an improved method for large scale production of proteins and/or polypeptides in cell culture is provided.
  • Fed-batch production involves the addition of small volumes of feed to supplement the nutrients present in the bioreactor as cell growth and product production progresses. It is understood that, in general, mammalian cells tend to continuously metabolize carbohydrates resulting in lactate accumulation, thus requiring base addition to neutralize the lactic acid. Base addition elevates osmolality in the cell medium which in turn greatly restricts the overall achievable cell viability and/or productivity in the bioreactor. Accumulation of lactate in the medium is detrimental to cell growth and is one of the common factors that limit the maximum productivity that can be achieved in batch culture.
  • lactate concentration in the culture reaches approximately 30-50 mM and/or ammonia concentration reaches 3-5 mM (Ozturk, S.S., Riley, M.R., and Palsson, B.O. 1992. Biotechnol. and Bioeng. 39: 418-431 ).
  • widely adopted schemes include nutrient supplementation and the design of chemically defined, serum-free media to support continuous cell growth and optimum product secretion.
  • Controlled feeding of cells is utilized in an effort to reach a more efficient metabolic phenotype (Europa, A. F., et al., 2000, Biotechnol. Bioeng. 67:25-34; Cruz et al., 1999, Biotechnol Bioeng, 66(2):104-1 13; Zhou et al., 1997, Cytotechnology 24, 99-108; Xie and Wang, 1994, Biotechnol Bioeng, 43: 1 174-89).
  • the invention provides cells and methods of culturing cells that have metabolically- shifted to lactate consumption. Metabolically adapted cells are ideal for large scale protein production.
  • One aspect of the invention is a method of culturing cells comprising transferring cells from a first cell culture to a second cell culture after a metabolic shift to lactate consumption in the cells has occurred in the first culture.
  • Another aspect of the invention provides a method of culturing cells comprising culturing cells in a first cell culture, determining that a metabolic shift to lactate consumption in the cells has occurred in the first cell culture, and transferring the cells to a second cell culture after the metabolic shift to lactate consumption in the cells has occurred, wherein lactate concentration in the second cell culture indicates net lactate consumption during the second culture.
  • the method further provides a decrease in accumulation of lactate in the second cell culture compared to that determined in an otherwise identical cell culture under otherwise identical conditions except transferring cells to the second cell culture is before a metabolic shift has occurred in the first cell culture.
  • a second aspect of the invention provides a method of producing a protein comprising transferring cells from a first cell culture to a second cell culture after a metabolic shift to lactate consumption in the cells has occurred, and maintaining the second cell culture for a period of time so that the protein accumulates in the cell culture.
  • the invention provides a method of producing a protein comprising culturing cells in a first cell culture, determining a metabolic shift to lactate consumption in the cells has occurred in the first cell culture, transferring the cells to a second cell culture after the metabolic shift to lactate consumption in the cells has occurred, and maintaining the second cell culture for a period of time so that the protein accumulates in the cell culture.
  • the method further provides an increase in productivity in the second cell culture compared to that determined in an otherwise identical cell culture under otherwise identical conditions except transferring cells to the second cell culture is before a metabolic shift has occurred in the first cell culture.
  • a third aspect of the invention provides an improved method of culturing cells, wherein the cells comprise a gene encoding a polypeptide of interest, comprising the steps of: culturing cells in a first cell culture, maintaining the first cell culture under conditions that allow the expansion of the cell mass, transferring the cells to a second cell culture after the metabolic shift to lactate consumption in the cells has occurred, maintaining the second cell culture under conditions that allow the expression of the polypeptide of interest, and harvesting the polypeptide of interest from the second cell culture.
  • the method further comprises determining a metabolic shift to lactate consumption in the cells has occurred in the first cell culture.
  • a fourth aspect of the invention provides an improved method of producing a polypeptide in a cell culture comprising the steps of: transfecting cells with DNA encoding a polypeptide of interest, culturing the cells in a first cell culture, transferring the cells to a second cell culture after the metabolic shift to lactate consumption in the cells has occurred, wherein the polypeptide of interest is expressed under conditions of a second cell culture, and maintaining the second cell culture for a period of time so that the polypeptide accumulates in the cell culture.
  • the method further comprises determining a metabolic shift to lactate consumption in the cells has occurred in the first cell culture.
  • a fifth aspect of the invention provides a method of producing a metabolically shifted cell line, comprising the steps of: maintaining a cell population in a first cell culture under conditions that allow the expansion of the cell mass, determining when a metabolic shift to lactate consumption in the cells has occurred, transferring a fraction of the cell population from the first cell culture to a second cell culture after the metabolic shift to lactate consumption in the cells has occurred, maintaining the cell population in the second cell culture for a period of time, and optionally harvesting the cells thus producing the metabolically shifted cell line.
  • Another aspect of the invention provides a metabolically shifted cell line produced by any of the methods of the invention disclosed herein.
  • the metabolically shifted cell comprises a nucleic acid sequence stably integrated into the cellular genome wherein the nucleic acid sequence encodes a polypeptide or protein of interest. In other embodiments, the metabolically shifted cell comprises an expression vector encoding a polypeptide or protein of interest.
  • the metabolic shift to lactate consumption is detected by pH, lactate or base measurements in the first cell culture. In other embodiments, the cells are transferred to a second cell culture when lactate consumption is detected. In still other embodiments, the metabolic shift to lactate consumption is detected after pH increases in the first cell culture medium without addition of base. In other embodiments, the metabolic shift to lactate consumption is detected when lactate levels plateau in the first cell culture.
  • the method further comprises determining the metabolic shift comprising: measuring pH in the first cell culture, adding base to maintain pH above a predetermined lower limit, determining that the pH is above the predetermined lower limit for consecutive intervals, and ceasing the addition of base, thereby determining that the metabolic shift to lactate consumption has occurred in the first cell culture.
  • the metabolic shift to lactate consumption is detected by indicators or products of cell metabolism, including but not limited to oxygen consumption, and metabolites such as glycine, tryptophan, phenylalanine, adenine, palmitic acid, glutamic acid, methionine and asparagine.
  • the metabolic shift to lactate consumption is detected by metabolomic analysis or proteomic analysis.
  • the metabolic shift occurs when the cells emerge from log (i.e. exponential growth) phase in the first cell culture.
  • the cells are transferred after the cells emerge from log phase in the first cell culture.
  • the metabolic shift occurs when the cells have reached stationary growth phase in the first cell culture.
  • the cells are transferred after the cells have reached stationary growth phase in the first cell culture.
  • the metabolic shift occurs in the first cell culture on or after 3 days of cell growth in the first cell culture. In another embodiment, the metabolic shift occurs in the first cell culture on or after 3.5 days of cell growth in the first cell culture.
  • the first cell culture is a seed culture.
  • the second cell culture is a fed-batch culture.
  • the second cell culture is a production culture.
  • the second cell culture is performed in a production bioreactor.
  • the cells are transferred to the second cell culture at a starting cell density of greater than or equal to about 0.5 x 10 6 cells/mL.
  • the cells are transferred to the second cell culture at a starting cell density between about 0.5-3.0 x 10 6 cells/mL.
  • lactate concentration in the second cell culture indicates net lactate consumption, for example, net lactate consumption is achieved on or after 2 days, 3 days, 4 days, or 5 days of cell growth in the second cell culture.
  • the decrease in accumulation of lactate is a reduction in peak lactate concentration in the second cell culture.
  • the reduction in peak lactate concentration occurs in the second cell culture on or after 5 days of cell growth in the second cell culture.
  • peak lactate concentration in the second cell culture is less than about 6 g/L, 5 g/L, 4 g/L, 3 g/L, 2 g/L, or less than about 1 g/L.
  • the cell or cells are selected from the group consisting of CHO, COS, retinal, Vero, CV1 , HEK293, 293 EBNA, MSR 293, MDCK, HaK, BHK21 , HeLa, HepG2, WI38, MRC 5, Colo25, HB 8065, HL-60, Jurkat, Daudi, A431 , CV-1 , U937, 3T3, L cell, C127 cell, SP2/0, NS-0, MMT, PER.C6, murine lymphoid, and murine hybridoma cells.
  • FIG. 1 A fusion protein-producing CHO cell line seed vessel was used to inoculate replicate production bioreactors at (Fig. 1A) three different metabolic states (online pH and offline lactate) and viable cell counts (VCC). Base usage normalized to 1 for the seed vessel is also shown. The parameters (time, pH, lactate, VCC, and base) for each cell culture (Condition #1 , #2, and #3) for which cells were transferred to production bioreactors is indicated by open rectangles (dotted line). All production bioreactors were run with the same operating conditions. The impact of each seed train and its metabolic state on protein titer (Fig. 1 B) and lactate (Fig. 1C) in a production bioreactor is shown. Production bioreactor trendlines represent the average of duplicate bioreactors with error bars that represent ⁇ one standard deviation.
  • FIG. 2 An antibody-producing CHO cell line seed vessel was used to inoculate replicate production bioreactors in a chemically defined process at (Fig. 2A) four different metabolic states (offline pH and lactate) and viable cell counts. The parameters (time, pH, lactate, and VCC) for each cell culture (Condition #1 , #2, #3 and #4) for which cells were transferred to production bioreactors is indicated by open rectangles (dotted lines). All production bioreactors were run with the same operating conditions. Condition #1 was lost after one week. The impact of each seed train and its metabolic state on a production bioreactor protein titer (Fig. 2B) and lactate accumulation (Fig. 2C) is also shown.
  • Production bioreactor trendlines represent the average of duplicate bioreactors with error bars that represent ⁇ one standard deviation.
  • Batch culture or "batch mode” as used herein is a phrase that refers to a unit (e.g. culturing vessel) that is filled with cells and with an initial full working volume of medium that is never exchanged.
  • all components for cell culturing are supplied to the culturing vessel at the start of the culturing process.
  • the culture usually runs until the nutrients are exhausted or the waste products reach toxic levels and the cells stop growing.
  • seed culture or “seed train” (also referred to as inoculum train) as used herein includes the inoculation source of a cell population which is allowed to expand in batch culture, or series of batch cultures, until ready for production scale.
  • the seed train expansion process constitutes the initial growth phase of the cells, or inoculum growth phase, following a thaw of frozen cells.
  • the interval between cell thawing and the accumulation of sufficient cell mass to inoculate a production bioreactor constitutes the seed train expansion phase.
  • the cell mass may be scaled up through several bioreactor stages in seed culture, and the cells are grown in cell culture medium under conditions favorable to the survival, growth and viability of the cell culture.
  • the seed train is intended to maximize the exponential growth phase, or achieve the maximal growth rate for the particular cell type being cultured. Therefore, passaging of cells from one bioreactor or vessel to another may be one way to achieve maximal growth rate.
  • the precise conditions will vary depending on the cell type, the organism from which the cell was derived, and the nature and character of the expressed polypeptide or protein.
  • a shift to lactate consumption metabolism may occur or be detected in any one of the vessels in a seed train expansion.
  • fed-batch cell culture or “fed-batch culture” when used herein refers to a batch culture wherein the animal cells and culture medium are supplied to the culturing vessel initially and additional culture nutrients are slowly fed, continuously or in discrete increments, to the culture during culturing, with or without periodic cell and/or product harvest before termination of culture.
  • Fed-batch culture includes "semi-continuous fed-batch culture” wherein periodically whole culture (which may include cells and medium) is removed and replaced by fresh medium.
  • Fed-batch culture is distinguished from simple “batch culture” whereas all components for cell culturing (including the animal cells and all culture nutrients) are supplied to the culturing vessel at the start of the culturing process in batch culture.
  • Fed-batch culture can be further distinguished from perfusion culturing insofar as the supernatant is not removed from the culturing vessel during the process, whereas in perfusion culturing, the cells are restrained in the culture by, e.g., filtration, and the culture medium is continuously or intermittently introduced and removed from the culturing vessel.
  • removal of samples for testing purposes during fed-batch cell culture is
  • the fed-batch process continues until it is determined that maximum working volume and/or protein production is reached.
  • continuous cell culture when used herein relates to a technique used to grow cells continually, usually in a particular growth phase. For example, if a constant supply of cells is required, or the production of a particular polypeptide or protein of interest is required, the cell culture may require maintenance in a particular phase of growth. Thus, the conditions must be continually monitored and adjusted accordingly in order to maintain the cells in that particular phase.
  • log phase means a period of cell growth typically characterized by cell doubling.
  • exposure growth phase or “exponential phase” are used interchangeably with log phase.
  • log phase the number of new cells appearing per unit of time is proportional to the present cell population, hence plotting the natural logarithm of cell number against time produces a straight line. If growth is not limited, doubling will continue at a constant rate so both the number of cells and the rate of population increase doubles with each consecutive time period.
  • stationary phase refers to the point where the rate of cell growth equals the rate of cell death.
  • the stationary phase is represented as a plateau, or “smooth,” horizontal linear part of the curve.
  • cell when used herein includes any cell that is suitable for expressing a recombinant nucleic acid sequence.
  • Cells include those of eukaryotes, such as non-human animal cells, mammalian cells, human cells, or cell fusions such as, for example, hybridomas or quadromas.
  • the cell is a human, monkey, ape, hamster, rat or mouse cell.
  • the cell is selected from the following cells: CHO (e.g. CHO K1 , DXB-1 1 CHO, Veggie-CHO), COS (e.g. COS-7), retinal cells, Vera, CV1 , kidney (e.g.
  • the cell comprises one or more viral genes, e.g. a retinal cell that expresses a viral gene (e.g. a PER.C6® cell).
  • the cell is a CHO cell. In other embodiments, the cell is a CHO K1 cell.
  • a "cell line” as used herein refers to a cell or cells that are derived from a particular lineage through serial passaging or subculturing of cells.
  • the term “cells” is used interchangeably with “cell population”.
  • CHO cells Given the current state-of-the-art feeding strategies, CHO cells have achieved cell numbers such as 1 1 * 10 6 cells/mL (at day 8) and titers of, for example, 2.3 g/L human IgG (harvested at day 14), numbers that are typical industrial values for CHO cell fed-batch cultures (Kim, BJ, et al. Biotechnol Bioeng. 2012 Jan; 109(1 ): 137-45. doi: 10.1002/bit.23289. Epub 201 1 Oct 3). Even more than 10 g/L production of antibody has been reported from CHO cells which have been well established as an important industrial mammalian cell line (Omasa et al, Current Pharmaceutical Biotechnology, 2010, 1 1 : 233-240).
  • cell culture medium and “culture medium” refer to a nutrient solution used for growing mammalian cells that typically provides the necessary nutrients to enhance growth of the cells, such as a carbohydrate energy source, essential amino acids, trace elements, vitamins, etc.
  • Cell culture medium may contain extracts, e.g. serum or peptones (hydrolysates), which supply raw materials that support cell growth.
  • Media may contain yeast-derived or soy extracts, instead of animal-derived extracts.
  • Chemically defined medium refers to a cell culture medium in which all of the chemical components are known. Chemically defined medium is entirely free of animal-derived components, such as serum- or animal-derived peptones.
  • One aspect of the invention relates to a growth phase wherein cell culture conditions are modified to enhance the growth of recombinant eukaryotic cells.
  • a basal culture medium and cells are supplied to a culturing vessel in batch.
  • the culturing vessel is inoculated with cells.
  • a suitable seeding density for the initial cell growth phase varies depending on the starting cell line, for example in the range of 0.2 to 3 x 10 6 cells/mL.
  • Culturing vessels include, but are not limited to well plates, T-flasks, shake flasks, stirred vessels, spinner flasks, hollow fiber, air lift bioreactors, and the like.
  • a suitable cell culturing vessel is a bioreactor.
  • a bioreactor refers to any culturing vessel that is manufactured or engineered to manipulate or control environmental conditions. Such culturing vessels are well known in the art.
  • Bioreactor processes and systems have been developed to optimize gas exchange, to supply sufficient oxygen to sustain cell growth and productivity, and to remove C0 2 .
  • Maintaining the efficiency of gas exchange is an important criterion for ensuring successful scale up of cell culture and protein production.
  • Such systems are well-known to the person having skill in the art.
  • the exponential growth phase or seed culture (i.e. first cell culture) is typically followed by a distinct second culture, known as the polypeptide production phase.
  • cells undergoing a metabolic shift to lactate consumption in a first cell culture are transferred to a second cell culture.
  • the second cell culture is carried out in a different culturing vessel from the cell growth phase or seed culture.
  • the second cell culture takes place in a production bioreactor.
  • transferring cells refers to the extraction of a fraction of the cell population from the first cell culture vessel and placing the cell population fraction into a second cell culture vessel to initiate the second cell culture.
  • transferring cells may refer to a volume of cells containing the cells of the first cell culture is placed in a different vessel and the inoculum volume is a fraction of the final volume of the second cell culture, for example about 20%, 30%, 40%, or 50%, or 60%, or 70% or 80% of the final volume.
  • transferring cells may refer to a volume of cells containing the cells of the first cell culture remain in the starting vessel and medium is added so that the initial volume (first cell culture) is a fraction of the final volume of the second cell culture.
  • the first cell culture is diluted, thereby transferring cells to a second cell culture.
  • Emerging from a particular phase includes the time period where measurements indicate that a first phase is slowing down or nearly complete, and the subsequent phase is beginning. Emerging from log phase, for example, indicates that cells are ending log phase, and/or are starting or have reached stationary phase. Growth phases are typically measured by viable cell concentration.
  • cell density refers to the number of cells per volume of sample, for example as number of total (viable and dead) cells per imL
  • the number of cells may be counted manually or by automation, such as with a flow cytometer. Automated cell counters have been adapted to count the number of viable or dead or both viable/dead cells using for example a standard tryptan blue uptake technique.
  • viable cell density or “viable cell concentration” refers to the number of viable cells per volume of sample (also referred to as “viable cell count”). Any number of well-known manual or automated techniques may be used to determine cell density. Online biomass measurements of the culture may be measured, where the capacitance or optical density is correlated to the number of cells per volume.
  • Final cell density in a first cell culture varies depending on the starting cell line, for example in the range of about 1 .0 to 10 x 10 6 cells/mL. In some embodiments, final seed train density reaches 1 .0 to 10 x 10 6 cells/mL prior to transfer of cells to a second cell culture. In other embodiments, final seed train density reaches 5.0 to 10 x 10 6 cells/mL prior to transfer of cells to a second cell culture.
  • a fraction of the cell population in the first cell culture is transferred to the second cell culture.
  • the cell population in the first cell culture is transferred to the second cell culture such that the first cell culture is a fraction of the second cell culture.
  • the starting cell density of the second culture may be chosen by the person of ordinary skill in the art. In some embodiments, the starting cell density in the second cell culture is between about 0.5 x 10 6 cells/mL to about 3.0 x 10 6 cells/mL.
  • the starting cell density in the second cell culture is about 0.5, 0.6, 0.7, 0.8, 0.9, 1.0, 1.1 , 1 .2, 1 .3, 1 .4, 1 .5, 1 .6, 1 7, 1 .8, 1 .9, 2.0, 2.1 , 2.2, 2.3, 2.4, 2.5, 2.6, 2.7, 2.8, 2.9, or 3.0 x 10 6 cells/mL.
  • the cell supernatant or cell lysate is harvested following the production phase.
  • the polypeptide or protein of interest is recovered from the culture medium or cell lysate, using techniques well known in the art.
  • the phrase "metabolic shift" when used herein refers to a change in cell metabolism, or use of carbon nutrient sources, from lactate production to net lactate consumption. While not being bound to any one theory, the most common carbon nutrient sources in serum-free media are glucose and glutamine, which support rapid cell growth. Glucose may be completely oxidized to C0 2 and H 2 0, or, based on the availability of oxygen, be converted to lactate such as in aerobic glycolysis. Fast growing cells consume glucose and glutamine quickly, leading to incomplete oxidative metabolism and, hence, excess lactate production. Carbohydrate metabolism may switch to lactate consumption, and thus reduce the accumulation of lactate.
  • lactate consumption when used herein refers to the use of lactate as a carbon source in cell metabolism.
  • the method of the invention is well-suited for preconditioning cells into a metabolically shifted state such that the cells may be used in any second or subsequent cell culture where lactate consumption is preferred.
  • overall accumulation of lactate decreases in the second cell culture.
  • net lactate consumption is achieved during the second cell culture, for example, net lactate consumption is achieved on or after 2 days, 3 days, 4 days, or 5 days of cell growth in the second cell culture.
  • the decrease in accumulation of lactate is a reduction in peak lactate concentration in the second cell culture.
  • the reduction in peak lactate concentration occurs in the second cell culture on or after 5 days of cell growth in the second cell culture.
  • peak lactate concentration in the second cell culture is less than about 6 g/L, 5 g/L, 4 g/L, 3 g/L, 2 g/L, or less than about 1 g/L.
  • metabolically shifted cells produce at least 2-fold, or 3-fold, or 4-fold, or 5-fold, or up to 10-fold lower lactate concentration values in a second cell culture.
  • lower lactate concentration values in a second cell culture or overall decreased accumulation of lactate in the second cell culture is compared to that determined in an otherwise identical cell culture under otherwise identical conditions except transferring cells to the second cell culture is before a metabolic shift has occurred in the first cell culture.
  • overall accumulation of lactate decreases in the second cell culture on or after 5 days of cell growth in the second cell culture.
  • overall product titer increases in the second cell culture.
  • metabolically shifted cells produce at least 2-fold, or 2.5-fold, 3-fold, or 4-fold, or 5-fold, or up to 10-fold higher product titer in a second cell culture.
  • higher protein titer values in a second cell culture is compared to that determined in an otherwise identical cell culture under otherwise identical conditions except transferring cells to the second cell culture is before a metabolic shift has occurred in the first cell culture.
  • Optimizing metabolic control of cells in culture prior to the fed-batch or production stage has many advantages.
  • Metabolic shift to lactate consumption in a first culture may be determined by multiple parameters. Determining a metabolic shift comprises a number of methods known to the skilled artisan for determining the metabolic state of growing cells.
  • Measurement of lactate concentration values in a first cell culture may be done by a variety of bioassay systems and kits well known to the person skilled in the art, such as analyzers using electrochemistry (e.g. Bioprofile® Flex, Nova Biomedical, Waltham, MA), or Raman spectroscopy, and may be used for offline or online monitoring of lactate
  • lactate accumulation has a detrimental effect on cell culture, and subsequently has a negative effect on protein product yield.
  • the metabolic shift is determined in a first cell culture when the net accumulation of lactate slows or ceases.
  • the metabolic shift to lactate consumption is detected by lactate measurements in the first cell culture.
  • the metabolic shift is determined in a first cell culture when a plateau, or essentially horizontal line, is determined on a graph representing the measurement of consecutive lactate concentration values in the culture.
  • the lactate concentration value remains below the upper tolerance limit for consecutive measurements.
  • the upper tolerance limit for lactate concentration is no greater than 4 g/L. It is understood that lactate levels plateau when the cells undergo net lactate consumption.
  • determining the metabolic shift comprises measuring lactate in the first cell culture at intervals, and determining that the lactate is below the
  • pH management and control is an important aspect of maintaining cells in a bioreactor culture.
  • the growth of most cells is optimal within narrow limits of pH.
  • cell culture is maintained at a neutral pH of 7.0, within a range of upper and lower set-point values. Set point values are determined by the person skilled in the art depending on the particular cell line in culture, the medium composition and the optimal conditions for growth for that cell.
  • neutral pH means a pH of about 6.85 to about 7.4.
  • neutral pH includes pH values of about 6.85, 6.9, 6.95, 7.0, 7.05, 7.1 , 7.15, 7.2, 7.25, 7.3, 7.35, and 7.4
  • On-line, or "real-time”, pH monitoring and addition of base may be accomplished by any number of methods well-known to the person skilled in the art.
  • real-time measurements of biological and chemical parameters in the cell culture by direct connection to an analyzer provide feedback in order to carry out additional actions, for example adding base or adding nutrients to the culture medium.
  • Off-line measurements may also be done whereas periodic sampling and manual operator intervention takes place.
  • Continuous measurement of pH allows cell medium to be monitored and base is added, for example, if acidity reaches a lower set point value outside of tolerance limits. If the pH reaches the set upper tolerance limits (i.e. becomes too basic), C0 2 may be added.
  • On-line monitoring may be done by a variety of methods. Electrodes, such as flow- through electrodes, are commonly used to measure pH, or other parameters such as dissolved 0 2 (d0 2 ) and temperature, in cell culture medium. Such flow-through electrodes plug directly into any standard strip chart recorder for continuous recording or can be interfaced to any standard laboratory pH or millivolt meter. pH may also be measured by means of an optical measurement with the use of a fluorescent sensor spot mounted in the bioreactor.
  • any such monitoring system will integrate a tolerance (or dead-band) limit around set point upper and lower values.
  • the dead-band prevents the dosing system from too rapidly switching on and off.
  • no dosing or titration will take place if the pH deviation from the set point is within the tolerance limits.
  • a liquid base e.g. KOH, NaOH, NaHC0 3
  • NH 3 gas e.g. NaOH, NaHC0 3
  • the pH measurement values are above the upper tolerance limit (basic), an acid or C0 2 gas will be added.
  • the pH set-point and control strategy e.g., dead- band
  • multiple parameters such as dissolved C0 2 , base consumption for pH control, and therefore, osmolality.
  • osmolality See e.g. Li, F., et al., 2010, mAbs 2(5):466-479.
  • the metabolic shift is determined in a first cell culture when addition (i.e. titration) of base stops.
  • Trending of base includes on-line trending wherein an automated monitoring method may be utilized to determine pH and the periodic addition of base.
  • the pH set points may vary but the rise in pH off the lower dead-band are indicative of metabolic shift in the first cell culture.
  • Online and manual methods of measuring base trending are known in the art, including methods to monitor the weight of the vessel, or the flow rate of the pump to detect base addition or stoppage of base addition.
  • the metabolic shift is determined in a first cell culture when the addition of base is no longer necessary to raise the pH above the lower tolerance limit.
  • the metabolic shift is determined in a first culture when the pH value increases without addition of base. In other embodiments, the pH value increases above the lower tolerance limit for consecutive measurements.
  • determining the metabolic shift comprises: (a) tuning a pH detection instrument to detect the noise level in the first cell culture, (b) continuously measuring pH in the first cell culture at regular intervals, (c) adding base as necessary to maintain pH above a predetermined lower limit, (d) determining that the pH is above the predetermined lower limit for several consecutive intervals, and (e) ceasing the addition of base, thereby determining that the metabolic shift to lactate consumption in the cells has occurred.
  • the lower tolerance limit is a pH of about 6.5, 6.55, 6.6, 6.65, 6.7, 6.75, 6.8, 6.85, 6.9, 6.95, 7.0, 7.05 or about 7.1.
  • the metabolic shift to lactate consumption is detected by indicators or products of cell metabolism in the first cell culture.
  • One such indicator of cell metabolism is oxygen consumption (Zagari, et al., 2013, New Biotechnol. 30(2):238-245).
  • An accurate measure of the rate of oxygen depletion in cell culture medium can be used to determine, the presence of viable cells in the culture following inoculation, as well as the rate of growth of the cells in culture (see, e.g., U.S. Patent No. 6,165,741 and U.S. Patent No. 7,575,890). Measurement of oxygen consumption is well-known in the art.
  • Other indicators of cell metabolism may be measured by proteomic or metabolomic techniques, such as immunological arrays, nuclear magnetic resonance (NMR) or mass spectometry.
  • Metabolites such as glycine, tryptophan, phenylalanine, adenine, palmitic acid, glutamic acid, methinonine and asparagine have been correlated with an increase of cellular biomass (See, e.g., Jain, M., et al, Science. 2012 May 25; 336(6084): 1040-1044.
  • the methods of the invention produce a protein or polypeptide of interest in a cell culture.
  • cells are engineered to recombinantly express the polypeptide or protein of interest.
  • Cells are transferred to a second cell culture, e.g. a production culture, after the metabolic shift to lactate consumption in the cells has occurred, and will be maintained in the second cell culture for a period of time so that the polypeptide or protein accumulates in the cell culture.
  • a second cell culture e.g. a production culture
  • a "polypeptide” is a single linear polymer chain of amino acids bonded together by peptide bonds between the carboxyl and amino groups of adjacent amino acid residues.
  • the term “protein” may also be used to describe a large polypeptide, such as a seven transmembrane spanning domain protein, with a particular folded or spatial structure. As such, the term “protein” is meant to include quaternary structures, ternary structures and other complex macromolecules composed of at least one polypeptide. If the protein is comprised of more than one polypeptide that physically associate with one another, then the term “protein” as used herein refers to the multiple polypeptides that are physically coupled and function together as the discrete unit. The term “protein” includes polypeptide.
  • polypeptides and proteins produced by the methods of the invention include antibodies, fusion proteins, Fc-fusion proteins, receptors, receptor-Fc fusion proteins, and the like.
  • immunoglobulin refers to a class of structurally related glycoproteins consisting of two pairs of polypeptide chains, one pair of light (L) chains and one pair of heavy (H) chains, which may all four be inter-connected by disulfide bonds.
  • L light
  • H heavy
  • each heavy chain typically comprises a heavy chain variable region (abbreviated herein as V H or VH) and a heavy chain constant region (C H ).
  • the heavy chain constant region typically comprises three domains, C H 1 , C H 2, and C H 3.
  • Each light chain typically comprises a light chain variable region (abbreviated herein as V L or VL) and a light chain constant region.
  • V L light chain variable region
  • the light chain constant region typically comprises one domain (C L ).
  • the V H and V L regions may be further subdivided into regions of hypervariability (or hypervariable regions which may be hypervariable in sequence and/or form of structurally defined loops), also termed complementarity determining regions (CDRs), interspersed with regions that are more conserved, termed framework regions (FRs).
  • CDRs complementarity determining regions
  • Each V H and V L is typically composed of three CDRs and four FRs, arranged from amino-terminus (N-terminus) to carboxy-terminus (C-terminus) in the following order: FR1 , CDR1 , FR2, CDR2, FR3, CDR3, FR4 (see also Chothia and Lesk J. Mol. Biol. 196, 901 -917 (1987)).
  • the numbering of amino acid residues in this region is according to IMGT, Sequences of Proteins of Immunological Interest, 5th Ed. Public Health Service, National Institutes of Health, Bethesda, MD. (1991 ), or by the EU numbering system of Kabat (also known as "EU numbering" or "EU index”), e.g. , as in Kabat, E.A. et al. Sequences of Proteins of Immunological interest. 5 ed. US Department of Health and Human Services, NIH publication No. 91-3242 (1991 ).
  • Fc refers to a portion of a heavy chain constant region that comprises at least the CH2 and CH3 domains that typically bind to an Fc receptor e.g., an FcyR, namely FcyRI (CD64), FcyRII (CD32), FcyRIII (CD16) or an FcRn, i.e., a neonatal Fc receptor.
  • an Fc-fusion protein may contain all or part of a native Fc domain or contain deletions, substitutions, and/or insertions or other modifications that render it unable to bind any Fc receptor, therefore rendering the domain non-functional or "effectorless" in terms of its typical biological function as achieved through an Fc receptor.
  • antibody refers to an immunoglobulin molecule, or a derivative thereof, which has the ability to specifically bind to an antigen.
  • the variable regions of the heavy and light chains of the immunoglobulin molecule contain a binding domain that interacts with an antigen as outlined above under "immunoglobulin".
  • An antibody may also be a bispecific antibody, diabody, or similar molecule (see for instance Holliger, et al., 1993, PNAS USA 90(14), 6444-8, for a description of diabodies). Further, it has been shown that the antigen-binding function of an antibody may be performed by fragments of a full-length antibody, i.e.
  • antigen-binding fragments or “antigen-binding proteins”.
  • antigen-binding proteins may be monospecific or multispecific (e.g., bispecific).
  • binding molecules or fragments encompassed within the term "antibody” include, but are not limited to (i) a Fab' or Fab fragment, a monovalent fragment consisting of the V L , V H , C L and C H 1 domains, or a monovalent antibody as described in the international patent publication number WO2007059782; (ii) F(ab') 2 fragments, bivalent fragments comprising two Fab fragments linked by a disulfide bridge at the hinge region; (iii) a Fd fragment consisting essentially of the V H and C H 1 domains; (iv) a Fv fragment consisting essentially of a V L and V H domains, (v) a dAb fragment (Ward et al., 1989, Nature 341 , 544-546), which consists essentially of a
  • monoclonal antibody or “monoclonal antibody composition” as used herein refer to a preparation of antibody molecules of single molecular composition.
  • a monoclonal antibody composition displays a single binding specificity and affinity for a particular epitope.
  • human antibody is intended to include antibodies having variable and constant regions derived from human germline immunoglobulin sequences.
  • Human antibodies may include amino acid residues not encoded by human germline immunoglobulin sequences (e.g., mutations introduced by random or site- specific mutagenesis in vitro or during gene rearrangement or by somatic mutation in vivo).
  • mouse or murine monoclonal antibody refers to antibodies displaying a single binding specificity which have variable and constant regions derived from murine or mouse germline immunoglobulin sequences.
  • fusion protein includes Fc fusion protein and receptor-Fc fusion protein.
  • a fusion protein may be any polypeptide formed by expression of a chimeric gene made by combining more than one DNA sequence of different origins, typically by cloning one gene into an expression vector in frame with a second gene such that the two genes are encoding one continuous polypeptide.
  • the invention provides a method described herein for producing a recombinant polypeptide or protein of interest.
  • the recombinant polypeptide or protein of interest is selected from the group consisting of an antibody, antigen-binding protein, fusion protein, Fc fusion protein, and receptor-Fc fusion protein.
  • a product according to the invention is a polypeptide, or a protein, which is expressed in the cells and is harvested from the cultivation system, i.e. the cells and/or the cell medium. It can be any polypeptide or protein of interest (supra).
  • Expression vectors typically use strong gene promoters to drive product mRNA transcription.
  • the invention relates to an expression vector encoding a polypeptide, e.g. an antibody, antigen-binding protein or fusion protein, of interest.
  • a polypeptide e.g. an antibody, antigen-binding protein or fusion protein
  • Such expression vectors may be used in the methods of the invention for recombinant production of polypeptides or proteins of interest via cell culture.
  • An expression vector in the context of the methods of the invention may be any suitable vector, including chromosomal, non-chromosomal, and synthetic nucleic acid vectors (a nucleic acid sequence comprising a suitable set of expression control elements).
  • suitable vectors include derivatives of SV40, bacterial plasmids, phage DNA, baculovirus, yeast plasmids, vectors derived from combinations of plasmids and phage DNA, and viral nucleic acid (RNA or DNA) vectors.
  • nucleic acid vectors and the usage thereof are well known in the art (see, for instance, US 5,589,466 and US 5,973,972).
  • a vector comprising a nucleic acid molecule encoding the polypeptide or protein of interest is provided in the host cell, wherein the nucleic acid molecule is operatively linked to an expression control sequence suitable for expression in a mammalian host cell.
  • Expression control sequences are engineered to control and drive the transcription of polypeptide-encoding genes of interest, and subsequent expression of polypeptides or proteins in various cell systems.
  • Plasmids combine an expressible gene of interest with expression control sequences (i.e. expression cassettes) that comprise desirable elements such as, for example, promoters, enhancers, selectable markers, operators, etc.
  • expression control sequences i.e. expression cassettes
  • desirable elements such as, for example, promoters, enhancers, selectable markers, operators, etc.
  • nucleic acid molecules may comprise or be associated with any suitable promoter, enhancer, selectable marker, operator, repressor protein, polyA termination sequences and other expression-facilitating elements.
  • Promoter indicates a DNA sequence sufficient to direct transcription of a DNA sequence to which it is operably linked, i.e., linked in such a way as to control transcription of nucleotide sequence.
  • the expression of a nucleotide sequence may be placed under control of any promoter or enhancer element known in the art. Examples of such elements include strong expression promoters (e. g., human CMV IE
  • CMV-MIE CMV major IE
  • the vector comprises a promoter selected from the group consisting of SV40, CMV, CMV-IE, CMV-MIE, RSV, SL3-3, MMTV, Ubi, UbC and HIV LTR.
  • Nucleic acid molecules encoding the polypeptide or protein of interest may also be operatively linked to an effective poly (A) termination sequence, an origin of replication for plasmid product in E. coli, an antibiotic resistance gene as selectable marker, and/or a convenient cloning site (e.g., a polylinker).
  • Nucleic acids may also comprise a regulatable inducible promoter (inducible, repressable, developmentally regulated) as opposed to a constitutive promoter such as CMV IE (the skilled artisan will recognize that such terms are actually descriptors of a degree of gene expression under certain conditions).
  • Selectable markers are elements well-known in the art. Under the selective conditions, only cells that express the appropriate selectable marker can survive. Commonly, selectable marker genes express proteins, usually enzymes, that confer resistance to various antibiotics in cell culture. In other selective conditions, cells that express a flourescent protein marker are made visible, and are thus selectable.
  • Embodiments include beta-lactamase (bla) (beta- lactam antibiotic resistance or ampicillin resistance gene or ampR), bis (blasticidin resistance acetyl transferase gene), bsd (blasticidin-S deaminase resistance gene), bsr (blasticidin-S resistance gene), Sh ble (Zeocin® resistance gene), hygromycin phosphotransferase (hpt) (hygromycin resistance gene), tetM (tetracycline resistance gene or tetR), neomycin phosphotransferase II (npt) (neomycin resistance gene or neoR), kanR (kanamycin resistance gene), and pac (puromycin resistance gene).
  • bla beta-lactamase
  • ampR ampicillin resistance gene
  • bis blasticidin resistance acetyl transferase gene
  • bsd blasticidin-S deaminase resistance gene
  • bsr blastici
  • Selectable (or selection) markers are typically utilized within stable cell line development.
  • the vector comprises one or more selectable marker genes selected from the group consisting of bla, bis, BSD, bsr, Sh ble, hpt, tetR, tetM, npt, kanR and pac.
  • the vector comprises one or more selectable marker genes encoding green fluorescent protein (GFP), enhanced green fluorescent protein (eGFP), cyano fluorescent protein (CFP), enhanced cyano fluorescent protein (eCFP), yellow fluorescent protein (YFP), or the like.
  • gene expression in eukaryotic cells may be tightly regulated using a strong promoter that is controlled by an operator that is in turn regulated by a regulatory fusion protein (RFP).
  • the RFP consists essentially of a transcription blocking domain, and a ligand-binding domain that regulates its activity.
  • operator indicates a DNA sequence that is introduced in or near a gene of interest in such a way that the gene may be regulated by the binding of the RFP to the operator and, as a result, prevents or allows transcription of the gene of interest.
  • operators in prokaryotic cells and bacteriophage have been well characterized (Neidhardt, ed. Escherichia coli and Salmonella; Cellular and Molecular Biology 2d. Vol 2 ASM Press, Washington D.C. 1996). These include, but are not limited to, the operator region of the LexA gene of E.
  • the transcription blocking domain of the RFP is a restriction enzyme, such as Notl
  • the operator is the recognition sequence for that enzyme.
  • the operator must be located adjacent to, or 3' to the promoter such that it is capable of controlling transcription by the promoter. For example, U.S. Pat. No. 5,972,650, which is incorporated by reference herein, specifies that tetO sequences be within a specific distance from the TATA box.
  • the operator is selected from the group consisting of tet operator (tetO), Notl recognition sequence, LexA operator, lactose operator, tryptophan operator and Arc operator (AO).
  • the repressor protein is selected from the group consisting of TetR, LexA, LacI, TrpR, Arc, LambdaCI and GAL4.
  • the transcription blocking domain is derived from a eukaryotic repressor protein, e.g. a repressor domain derived from GAL4.
  • cells are engineered to express the tetracycline repressor protein (TetR) and a polypeptide of interest is placed under transcriptional control of a promoter whose activity is regulated by TetR.
  • TetR tetracycline repressor protein
  • Two tandem TetR operators tetO
  • TetR Two tandem TetR operators
  • Transcription of the gene encoding the protein of interest directed by the CMV- MIE promoter in such vector may be blocked by TetR in the absence of tetracycline or some other suitable inducer (e.g. doxycycline).
  • TetR protein In the presence of an inducer, TetR protein is incapable of binding tetO, hence transcription and thus translation (expression) of the polypeptide of interest occurs.
  • an inducer See, e.g. , US Patent No. 7,435,553, which is herein incorporated by reference in its entirety.
  • Such cell expression sytems may be used to "turn on" production of the polypeptide of interest during production culture only.
  • antibiotics such as a tetracycline or other suitable inducers, may be added to the bioreactor to a first cell culture.
  • Another exemplary cell expression system includes regulatory fusion proteins such as TetR-ER L BDT2 fusion protein, in which the transcription blocking domain of the fusion protein is TetR and the ligand-binding domain is the estrogen receptor ligand-binding domain (ER L BD) with T2 mutations (ER L BDT2; Feil et al., 1997, Biochem. Biophys. Res.
  • tetO sequences were placed downstream and proximal to the strong CMV-MIE promoter, transcription of the nucleotide sequence of interest from the CMV-MIE/fefO promoter was blocked in the presence of tamoxifen and unblocked by removal of tamoxifen.
  • fusion protein Arc2-ER L BoT2 a fusion protein consisting of a single chain dimer consisting of two Arc proteins connected by a 15 amino acid linker and the ER L BDT2 (supra), involves an Arc operator (AO), more specifically two tandem arc operators immediately downstream of the CMV-MIE promoter/enhancer.
  • Cell lines may be regulated by Arc2-ER L BDT2, wherein cells expressing the protein of interest are driven by a CMV-MIE/Arc02 promoter and are inducible with the removal of tamoxifen.
  • the vector comprises a CMV-MIE/TetO or CMV-MIE/A02 hybrid promoter.
  • Suitable vectors used in the methods of the invention may also employ Cre- /ox tools for recombination technology in order to facilitate the replication of a gene of interest.
  • a Cre-/ox strategy requires at least two components: 1 ) Cre recombinase, an enzyme that catalyzes recombination between two loxP sites; and 2) loxP sites (e.g. a specific 34-base pair bp sequence consisting of an 8-bp core sequence, where
  • yeast-derived FLP recombinase may be utilized with the consensus sequence FRT (see also, e.g. Dymecki, S., 1996, PNAS 93(12): 6191 -6196).
  • a gene i.e. a nucleotide sequence encoding a
  • recombinant polypeptide of interest is inserted within an expression-enhancing sequence of the expression cassette, and is optionally operably linked to a promoter, wherein the promoter-linked gene is flanked 5' by a first recombinase recognition site and 3' by a second recombinase recognition site.
  • a promoter-linked gene is flanked 5' by a first recombinase recognition site and 3' by a second recombinase recognition site.
  • a second promoter-linked gene is downstream (3') of the first gene and is flanked 3' by the second recombinase recognition site.
  • a second promoter-linked gene is flanked 5' by the second recombinase site, and flanked 3' by a third recombinase recognition site.
  • the recombinase recognition sites are selected from a loxP site, a /ox51 1 site, a /ox2272 site, and a FRT site.
  • the recombinase recognition sites are different.
  • the host cell comprises a gene capable of expressing a Cre recombinase.
  • the vector comprises a first gene encoding a light chain of an antibody or a heavy chain of an antibody of interest, and a second gene encoding a light chain of an antibody or a heavy chain of an antibody of interest.
  • one or more vectors carrying one or more nucleic acid sequences encoding for and expressing the protein of interest may be employed in such an expression system.
  • Cells of the invention may also be engineered to increase product expression via coexpression of proteins such as chaperones, apoptosis inhibitors, protein degradation inhibitors, or other protein which may enhance the expression or stability of the product.
  • proteins such as chaperones, apoptosis inhibitors, protein degradation inhibitors, or other protein which may enhance the expression or stability of the product.
  • the vector further comprises an X-box-binding-protein 1 (mXBP1 ) and/or an EDEM2 gene capable of enhancing protein production/protein secretion through control of the expression of genes involved in protein folding in the endoplasmic reticulum (ER).
  • mXBP1 X-box-binding-protein 1
  • EDEM2 EDEM2 gene capable of enhancing protein production/protein secretion through control of the expression of genes involved in protein folding in the endoplasmic reticulum (ER).
  • transiently transfected cells which produce rapidly significant quantities of the product may also be carried out for the optimization of a cell culture process, however stable transfection is typically utilized for production scales of large volume.
  • the metabolically shifted cell may contain any or all of the elements of a cell expression system as described herein necessary for the efficient recombinant production of a protein of interest.
  • the invention relates to a metabolically shifted recombinant eukaryotic host cell which produces a protein of interest.
  • host cells include mammalian cells, such as CHO, PER.C6, murine lymphoid, and murine hybridoma cell lines ⁇ supra).
  • the present invention provides a metabolically shifted cell comprising a nucleic acid sequence stably integrated into the cellular genome that comprises a sequence encoding for a protein of interest.
  • the present invention provides a metabolically shifted cell comprising a non- integrated (i.e., episomal) nucleic acid sequence, such as a plasmid, cosmid, phagemid, or linear expression element, which comprises a sequence encoding for a protein of interest.
  • a non- integrated (i.e., episomal) nucleic acid sequence such as a plasmid, cosmid, phagemid, or linear expression element, which comprises a sequence encoding for a protein of interest.
  • “Harvesting” or “cell harvesting” takes place at the end of a production batch in an upstream process.
  • Cells are separated from medium by a number of methods such as filtration, cell encapsulation, cell adherence to microcarriers, cell sedimentation or centrifugation. Purification of protein takes place in additional steps to isolate the protein product.
  • Polypeptides or proteins may be harvested from either the cells or cell culture media.
  • Protein purification strategies are well-known in the art. Soluble forms of the polypeptide, such as antibodies, antibody-binding fragments and Fc-containing proteins, may be subjected to commercially available concentration filters, and subsequently affinity purified by well-known methods, such as affinity resins, ion exchange resins,
  • Membrane-bound forms of the polypeptide can be purified by preparing a total membrane fraction from the expressing cell and extracting the membranes with a nonionic detergent such as TRITON® X-100 (EMD Biosciences, San Diego, CA, USA). Cytosolic or nuclear proteins may be prepared by lysing the host cells (via mechanical force, sonication, detergent, etc.), removing the cell membrane fraction by centrifugation, and retaining the supernatant.
  • a nonionic detergent such as TRITON® X-100
  • the invention relates to a method for producing an antibody, or antigen-binding protein, or fusion protein of interest, said method comprising the steps of a) culturing cells according to the method as described herein above, b) harvesting the cells, and c) purifying the polypeptide or protein, such as antibody, or antigen-binding protein, or fusion protein, from the cells or cell culture media.
  • Example 1- Determining metabolic shift parameters: Fusion protein-producing cell line
  • CHO cells were transfected with DNA expressing a fusion protein.
  • the fusion protein-producing CHO cell line was incubated in a seed vessel culture, in proprietary media containing soy, and parameters such as online pH, offline lactate and viable cell count, were measured and recorded to determine metabolic state (see #1 , #2, or #3 of Figure 1 A). Base usage was also monitored and normalized to 1 for this cell line (also see Figure 1A).
  • Cells under condition #1 and condition #2 were used to inoculate replicate production bioreactors when the pH was controlling at the bottom end of the control range and lactate and VCC were increasing.
  • Cells under condition #3 were inoculated when the pH was starting to increase off the bottom of the control range, i.e. base usage had stopped, indicating lactate remetabolization (i.e. consumption).
  • Cell growth in condition #3 had entered post-exponential growth phase. All production bioreactors were run with the same operating conditions.
  • Condition #3 cells had the most significant effect on the productivity and lactate accumulation in the second cell culture, resulting in a greater than 2-fold increase in product titer (compared to Conditions #1 and #2), in the production bioreactor (see Fig. 1 B). Condition #3 cells also resulted in decreased lactate concentration following transfer to the second cell culture (compared to Conditions #1 and #2- see Fig. 1 C). Condition #3 cells have a lactate profile indicative of net lactate consumption (see Fig. 1 C at 8-12 days of cell culture). Cells transferred from the first culture under Condition #1 (i.e. prior to a metabolic shift in first culture) do not achieve net lactate consumption in the production bioreactor.
  • An antibody-producing CHO cell line seed vessel was used to inoculate replicate production bioreactors similar to Example 1 , however in chemically defined medium.
  • Four different metabolic states were measured (monitoring offline pH, lactate and viable cell counts- see #1 , #2, #3, and #4 of Figure 2A).
  • VCC continued to increase during the duration of the seed vessel incubation when production bioreactors were inoculated.
  • Condition #1 was inoculated very early in the seed train when the pH was still at the top end of the control range and when the lactate was low but increasing.
  • Condition #2 was inoculated when the pH was starting to decrease and lactate was increasing and approaching peak levels.
  • Condition #3 was inoculated when the pH was near the bottom of the control range and lactate levels had plateaued.
  • Condition #4 was inoculated when the pH was starting to increase off the bottom of the control range and during lactate remetabolization (i.e. lactate consumption). All production bioreactors were run with the same operating conditions.
  • Condition #1 was lost after one week.
  • the impact of seed train metabolic state on production bioreactor titer ( Figure 2B) and lactate ( Figure 2C) profiles was determined. Production bioreactor trendlines represent the average of duplicate bioreactors with error bars that represent ⁇ one standard deviation.
  • Condition #3 and #4 cells had the most significant effect on the productivity in the second cell culture.
  • Condition #3 and #4 cells also resulted in reduced lactate concentration in the production bioreactor (compared to Conditions #1 and #2), which is indicative of a metabolic phenotype for lactate consumption (see Fig. 2B and 2C).
  • cells transferred from first culture under Condition #1 do not achieve net lactate consumption during the production phase.
  • Conditions #2, #3 and #4 achieve net lactate consumption during the production phase, however Condition #4 is most optimal since net lactate consumption occurs earlier than the other conditions, and the peak lactate level is the lowest.

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  • Molecular Biology (AREA)
  • Cell Biology (AREA)
  • Biophysics (AREA)
  • Immunology (AREA)
  • Medicinal Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Reproductive Health (AREA)
  • Micro-Organisms Or Cultivation Processes Thereof (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
  • Apparatus Associated With Microorganisms And Enzymes (AREA)
  • Peptides Or Proteins (AREA)

Abstract

La présente invention concerne un procédé amélioré de production à grande échelle de protéines et/ou de polypeptides dans une culture cellulaire. Selon la présente invention, le procédé consiste à cultiver des cellules ayant un métabolisme amélioré. L'utilisation d'un tel procédé ou d'un tel système permet de produire des taux élevés de protéines ou de polypeptides et de réduire l'accumulation de déchets métaboliques non souhaités tels que le lactate. Les protéines et les polypeptides exprimés selon la présente invention peuvent être utilisés de manière avantageuse dans la préparation de compositions pharmaceutiques, immunogènes, ou autres compositions biologiques commerciales, telles que des anticorps.
PCT/US2014/059993 2013-10-11 2014-10-10 Culture cellulaire à métabolisme optimisé WO2015054554A1 (fr)

Priority Applications (29)

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JP2016547976A JP6663854B2 (ja) 2013-10-11 2014-10-10 代謝が最適化された細胞培養
KR1020217011547A KR102358807B1 (ko) 2013-10-11 2014-10-10 대사적으로 최적화된 세포 배양
ES14851841.8T ES2678945T3 (es) 2013-10-11 2014-10-10 Cultivos celulares optimizados metabólicamente
SG11201601681QA SG11201601681QA (en) 2013-10-11 2014-10-10 Metabolically optimized cell culture
PL18161278T PL3351620T3 (pl) 2013-10-11 2014-10-10 Hodowla komórek zoptymalizowana metabolicznie
MX2020011334A MX2020011334A (es) 2013-10-11 2014-10-10 Cultivo celular metabolicamente optimizado.
MX2016004564A MX2016004564A (es) 2013-10-11 2014-10-10 Cultivo celular metabolicamente optimizado.
EA201690600A EA033783B1 (ru) 2013-10-11 2014-10-10 Метаболически оптимизированная клеточная культура
EP14851841.8A EP3055409B1 (fr) 2013-10-11 2014-10-10 Culture cellulaire à métabolisme optimisé
EP18161278.9A EP3351620B1 (fr) 2013-10-11 2014-10-10 Culture cellulaire à métabolisme optimisé
US15/028,521 US20160244725A1 (en) 2013-10-11 2014-10-10 Metabolically optimized cell culture
CA2926049A CA2926049C (fr) 2013-10-11 2014-10-10 Culture cellulaire a metabolisme optimise
DK14851841.8T DK3055409T3 (en) 2013-10-11 2014-10-10 METABOLIC OPTIMIZED CELL CULTURE
CN202210497778.2A CN114717196A (zh) 2013-10-11 2014-10-10 代谢优化的细胞培养物
AU2014331776A AU2014331776B2 (en) 2013-10-11 2014-10-10 Metabolically optimized cell culture
KR1020237008467A KR102610425B1 (ko) 2013-10-11 2014-10-10 대사적으로 최적화된 세포 배양
KR1020167009163A KR102243980B1 (ko) 2013-10-11 2014-10-10 대사적으로 최적화된 세포 배양
CN201480055499.4A CN105637085A (zh) 2013-10-11 2014-10-10 代谢优化的细胞培养物
EP20193898.2A EP3812453A1 (fr) 2013-10-11 2014-10-10 Culture cellulaire à métabolisme optimisé
PL14851841T PL3055409T3 (pl) 2013-10-11 2014-10-10 Metabolicznie zoptymalizowana hodowla komórkowa
KR1020227003381A KR102510238B1 (ko) 2013-10-11 2014-10-10 대사적으로 최적화된 세포 배양
ZA2016/01550A ZA201601550B (en) 2013-10-11 2016-03-04 Metabolically optimized cell culture
IL244511A IL244511A0 (en) 2013-10-11 2016-03-08 Cell culture in a metabolically optimal manner
US15/130,780 US20160244726A1 (en) 2013-10-11 2016-04-15 Metabolically optimized cell culture
HK16111206.9A HK1223122A1 (zh) 2013-10-11 2016-09-23 代謝優化的細胞培養物
IL262833A IL262833A (en) 2013-10-11 2018-11-06 Metabolically enriched cell culture
US16/984,531 US20210087535A1 (en) 2013-10-11 2020-08-04 Metabolically optimized cell culture
AU2021200193A AU2021200193B2 (en) 2013-10-11 2021-01-14 Metabolically optimized cell culture
US17/843,121 US20220315644A1 (en) 2013-10-11 2022-06-17 Metabolically optimized cell culture

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US201361889815P 2013-10-11 2013-10-11
US61/889,815 2013-10-11

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US15/130,611 Continuation-In-Part US11390663B2 (en) 2013-10-11 2016-04-15 Metabolically optimized cell culture
US16/984,531 Continuation US20210087535A1 (en) 2013-10-11 2020-08-04 Metabolically optimized cell culture

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KR (4) KR102510238B1 (fr)
CN (2) CN105637085A (fr)
AU (2) AU2014331776B2 (fr)
CA (1) CA2926049C (fr)
DK (2) DK3351620T3 (fr)
EA (2) EA201991976A1 (fr)
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HK (2) HK1223122A1 (fr)
HU (2) HUE039551T2 (fr)
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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160244726A1 (en) * 2013-10-11 2016-08-25 Regeneron Pharmaceuticals, Inc. Metabolically optimized cell culture
EP3351620B1 (fr) 2013-10-11 2020-09-02 Regeneron Pharmaceuticals, Inc. Culture cellulaire à métabolisme optimisé
US11390663B2 (en) 2013-10-11 2022-07-19 Regeneron Pharmaceuticals, Inc. Metabolically optimized cell culture

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP7260018B2 (ja) * 2017-03-31 2023-04-18 株式会社三洋物産 遊技機
JP7260011B2 (ja) * 2017-03-31 2023-04-18 株式会社三洋物産 遊技機
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US11609120B2 (en) 2017-10-06 2023-03-21 Lonza Ltd Automated control of cell culture using Raman spectroscopy
CA3075679A1 (fr) 2017-10-16 2019-04-25 Regeneron Pharmaceuticals, Inc. Bioreacteur a perfusion et procedes d'utilisation associes
JP7471220B2 (ja) * 2017-11-30 2024-04-19 エフ・ホフマン－ラ・ロシュ・アクチェンゲゼルシャフト 哺乳動物細胞の培養方法
GB201810772D0 (en) * 2018-06-29 2018-08-15 Ge Healthcare Bio Sciences Ab Method in bioprocess purification system
JP7231355B2 (ja) * 2018-08-22 2023-03-01 日機装株式会社 細胞培養方法および細胞培養装置
JP2020151560A (ja) * 2020-06-24 2020-09-24 株式会社三洋物産 遊技機
JP2020151559A (ja) * 2020-06-24 2020-09-24 株式会社三洋物産 遊技機

Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5589466A (en) 1989-03-21 1996-12-31 Vical Incorporated Induction of a protective immune response in a mammal by injecting a DNA sequence
US5972650A (en) 1997-06-26 1999-10-26 Brigham And Women's Hospital Tetracycline repressor regulated mammalian cell transcription and viral replication switch
US5973972A (en) 1995-11-03 1999-10-26 Samsung Electronics, Co., Ltd. Precharge system for a semiconductor memory device
US6165741A (en) 1997-05-30 2000-12-26 The Trustees Of The University Of Pennsylvania Method for rapid detection of bacterial growth in cultures
WO2004104186A1 (fr) 2003-05-15 2004-12-02 Wyeth Alimentation de glucose restreinte pour culture de cellules animales
WO2007059782A1 (fr) 2005-11-28 2007-05-31 Genmab A/S Anticorps monovalents recombines et leurs procedes de production
US7390660B2 (en) 2002-03-05 2008-06-24 Hoffman-La Roche Inc. Methods for growing mammalian cells in vitro
US7435553B2 (en) 2001-01-16 2008-10-14 Regeneron Pharmaceuticals, Inc. Isolating cells expressing secreted proteins
US20090162901A1 (en) 2002-05-29 2009-06-25 Regeneron Pharmaceuticals, Inc. Inducible Eukaryotic Expression System
US7575890B2 (en) 2006-01-18 2009-08-18 Oxygen Enterprises, Ltd. Method for rapid detection and evaluation of cultured cell growth
US20100291626A1 (en) 2007-06-04 2010-11-18 Regeneron Pharmaceuticals, Inc. Enhanced expression and stability regions
US8192951B2 (en) 2006-11-03 2012-06-05 Wyeth Llc Glycolysis-inhibiting substances in cell culture
US8470552B2 (en) 2009-10-12 2013-06-25 Keck Graduate Institute Strategy to reduce lactic acid production and control PH in animal cell culture

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6953692B2 (en) * 2001-12-18 2005-10-11 Bayer Pharmaceuticals Corporation Device and method for seed-train expansion of mammalian cells
US7039770B1 (en) 2002-03-05 2006-05-02 Juniper Networks, Inc. Low latency request dispatcher
US7531327B2 (en) * 2004-07-23 2009-05-12 Immunomedics, Inc. Methods and compositions for increasing longevity and protein yield from a cell culture
TWI374935B (en) 2004-08-27 2012-10-21 Pfizer Ireland Pharmaceuticals Production of α-abeta
TWI364458B (en) * 2004-08-27 2012-05-21 Wyeth Res Ireland Ltd Production of tnfr-lg
CN101300342A (zh) * 2005-11-02 2008-11-05 惠氏公司 用于使哺乳动物细胞具备适应性的方法
US20090042253A1 (en) 2007-08-09 2009-02-12 Wyeth Use of perfusion to enhance production of fed-batch cell culture in bioreactors
EA019812B1 (ru) * 2008-06-13 2014-06-30 Сентокор Орто Байотек Инк. Способы получения высокой плотности жизнеспособных клеток в культуре клеток млекопитающих
PL2563904T3 (pl) * 2010-04-26 2015-06-30 Novartis Ag Udoskonalona pożywka do hodowli komórkowej
EP2576580B1 (fr) * 2010-05-28 2016-09-14 F.Hoffmann-La Roche Ag Réduction du niveau de lactate et augmentation de la production de polypeptides par régulation négative de l'expression de la lactate déshydrogénase et de la pyruvate déshydrogénase kinase
TWI637057B (zh) 2012-11-09 2018-10-01 拜爾沙納有限公司 具交替生物反應器用途之不連續進料批次製程
MX2016004564A (es) 2013-10-11 2016-07-12 Regeneron Pharma Cultivo celular metabolicamente optimizado.

Patent Citations (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5589466A (en) 1989-03-21 1996-12-31 Vical Incorporated Induction of a protective immune response in a mammal by injecting a DNA sequence
US5973972A (en) 1995-11-03 1999-10-26 Samsung Electronics, Co., Ltd. Precharge system for a semiconductor memory device
US6165741A (en) 1997-05-30 2000-12-26 The Trustees Of The University Of Pennsylvania Method for rapid detection of bacterial growth in cultures
US5972650A (en) 1997-06-26 1999-10-26 Brigham And Women's Hospital Tetracycline repressor regulated mammalian cell transcription and viral replication switch
US7435553B2 (en) 2001-01-16 2008-10-14 Regeneron Pharmaceuticals, Inc. Isolating cells expressing secreted proteins
US7390660B2 (en) 2002-03-05 2008-06-24 Hoffman-La Roche Inc. Methods for growing mammalian cells in vitro
US20090162901A1 (en) 2002-05-29 2009-06-25 Regeneron Pharmaceuticals, Inc. Inducible Eukaryotic Expression System
WO2004104186A1 (fr) 2003-05-15 2004-12-02 Wyeth Alimentation de glucose restreinte pour culture de cellules animales
WO2007059782A1 (fr) 2005-11-28 2007-05-31 Genmab A/S Anticorps monovalents recombines et leurs procedes de production
US7575890B2 (en) 2006-01-18 2009-08-18 Oxygen Enterprises, Ltd. Method for rapid detection and evaluation of cultured cell growth
US8192951B2 (en) 2006-11-03 2012-06-05 Wyeth Llc Glycolysis-inhibiting substances in cell culture
US20100291626A1 (en) 2007-06-04 2010-11-18 Regeneron Pharmaceuticals, Inc. Enhanced expression and stability regions
US8470552B2 (en) 2009-10-12 2013-06-25 Keck Graduate Institute Strategy to reduce lactic acid production and control PH in animal cell culture

Non-Patent Citations (48)

* Cited by examiner, † Cited by third party
Title
"Cellular and Molecular Biology", vol. 2, 1996, ASM PRESS, article "Escherichia coli and Salmonella"
"Fundamental Immunology", 1989, RAVEN PRESS
"Sequences of Proteins of Immunological Interest", 1991, PUBLIC HEALTH SERVICE, NATIONAL INSTITUTES OF HEALTH
A. F. ET AL., BIOTECHNOL. BIOENG., vol. 67, 2000, pages 25 - 34
ARAKI ET AL., NUC ACIDS RES, vol. 30, no. 19, 2002, pages E103
ARAKI ET AL., PNAS, vol. 92, 1995, pages 160 - 4
BLECKWENN, NA; SHILOACH, J.: "Large-scale cell culture", CURR PROTOC IMMUNOL., vol. 59, 2004
CHOTHIA; LESK, J. MOL. BIOL., vol. 196, 1987, pages 901 - 917
CRUZ ET AL., BIOTECHNOL BIOENG, vol. 66, no. 2, 1999, pages 104 - 113
DE LA LUZ-HDEZ, K.: "Metabolomics and Mammalian Cell Culture", METABOLOMICS, 2012, ISBN: 978-953-51-0046-1
DYMECKI, S., PNAS, vol. 93, no. 12, 1996, pages 6191 - 6196
FEIL ET AL., BIOCHEM. BIOPHYS. RES. COMMUN., vol. 237, 1997, pages 752 - 757
GAMBHIR, A. ET AL., J BIOSCIENCE BIOENG, vol. 95, no. 4, 2003, pages 317 - 327
HOLLIGER ET AL., PNAS USA, vol. 90, no. 14, 1993, pages 6444 - 8
HOLT ET AL., TRENDS BIOTECHNOL., vol. 21, no. 11, 2003, pages 484 - 90
JAIN, M. ET AL., SCIENCE, vol. 336, no. 6084, 25 May 2012 (2012-05-25), pages 1040 - 1044
KABAT, E.A. ET AL.: "US Department of Health and Human Services", 1991, NIH, article "Sequences of Proteins of Immunological interest"
KIM, S.H.; LEE, G.M., APPL. MICROBIOL. BIOTECHNOL., vol. 74, 2007, pages 152 - 159
KIM, S.H.; LEE, G.M., APPL. MICROBIOL. BIOTECHNOL., vol. 76, 2007, pages 659 - 665
KIM; BJ ET AL., BIOTECHNOL BIOENG., vol. 109, no. 1, January 2012 (2012-01-01), pages 137 - 45
LE H. ET AL.: "discloses multivariate analysis of cell culture bioprocess data and lactate consumption as process indicator", J BIOTECHNOL., vol. 162, no. 2-3, 2012, pages 210 - 23
LE, H. ET AL.: "Multivariate analysis of cell culture bioprocess data - lactate consumption as process indicator", JOURNAL OF BIOTECHNOLOGY, vol. 162, no. 2-3, 2012, pages 210 - 223, XP055287323 *
LI F. ET AL.: "discloses cell culture processes for monoclonal antibody production", MABS., vol. 2, no. 5, 2010, pages 466 - 79, XP055166177, DOI: doi:10.4161/mabs.2.5.12720
LI, F. ET AL., MABS, vol. 2, no. 5, 2010, pages 466 - 479
MA N. ET AL.: "discloses a single nutrient feed supports both chemically defined NSO and CHO fed-batch processes: Improved productivity and lactate metabolism", BIOTECHNOL PROG., vol. 25, no. 5, 2009, pages 1353 - 63
MA, N. ET AL.: "A single nutrient feed supports both chemically defined NSO and CHO fed-batch processes: improved productivity and lactate metabolism", BIOTECHNOLOGY PROGRESS, vol. 25, no. 5, 2009, pages 1353 - 1363, XP055287324 *
MULUKUTLA B.C. ET AL.: "discloses on metabolic shift to lactate consumption in fed-batch culture", METAB ENG., vol. 14, no. 2, 2011, pages 138 - 49, XP028466094, DOI: doi:10.1016/j.ymben.2011.12.006
NAGY, A ET AL., GENESIS, vol. 26, 2000, pages 99 - 109
NEWLAND ET AL., BIOTECHNOL. BIOENG., vol. 43, no. 5, 1994, pages 434 - 8
OLIVARI ET AL., J. BIOL. CHEM., vol. 280, no. 4, 2005, pages 2424 - 2428
OMASA ET AL., CURRENT PHARMACEUTICAL BIOTECHNOLOGY, vol. 11, 2010, pages 233 - 240
OZTURK, S.S.; RILEY, M.R.; PALSSON, B.O., BIOTECHNOL. AND BIOENG., vol. 39, 1992, pages 418 - 431
QUEK ET AL., METAB ENG, vol. 12, no. 2, 2010, pages 161 - 71
REVETS ET AL., EXPERT OPIN BIOL THER, vol. 5, no. 1, 2005, pages 111 - 24
RON D; WALTER P., NAT REV MOL CELL BIOL., vol. 8, 2007, pages 519 - 529
SHEIKHOLESLAMI Z. ET AL.: "discloses the impact of the timing of induction on the metabolism and productivity of CHO cells in culture", BIOCHEM ENG J., vol. 79, 2013, pages 162 - 171, XP028733030, DOI: doi:10.1016/j.bej.2013.07.015
SHEIKHOLESLAMI, Z. ET AL.: "The impact of the timing of induction on the metabolism and productivity of CHO cells in culture", BIOCHEMICAL ENGINEERING JOURNAL, vol. 79, 2013, pages 162 - 171, XP028733030 *
VEMBAR; BRODSKY, NAT. REV. MOL. CELL. BIOL., vol. 9, no. 12, 2008, pages 944 - 957
WARD ET AL., NATURE, vol. 341, 1989, pages 544 - 546
WLASCHIN, K.F; HU, W-S., J. BIOTECHNOL., vol. 131, 2007, pages 168 - 176
XIE; WANG, BIOTECHNOL BIOENG, vol. 43, 1994, pages 1174 - 89
XIE; WANG, BIOTECHNOL. BIOENG., vol. 43, no. 11, 1994, pages 1175 - 1189
YOUNG D.J.: "discloses metabolic flux rewiring in mammalian cell cultures", CURR OPIN BIOTECHNOL., vol. 24, no. 6, 2013, pages 1108 - 1115, XP055295214, DOI: doi:10.1016/j.copbio.2013.04.016
ZAGARI ET AL., NEW BIOTECHNOL., vol. 30, no. 2, 2013, pages 238 - 245
ZAGARI ET AL., NEW BIOTECHNOL., vol. 30, no. 2, 2013, pages 238 - 45
ZAGARI F. ET AL.: "discloses lactate metabolism shift in CHO cell culture and the role of mitochondrial oxidative activity", N BIOTECHNOL., vol. 30, no. 2, 2013, pages 238 - 45, XP055295213, DOI: doi:10.1016/j.nbt.2012.05.021
ZHOU ET AL., CYTOTECHNOLOGY, vol. 24, 1997, pages 99 - 108
ZHOU W. ET AL.: "discloses fed-batch culture of recombinant NSO myeloma cells with high monoclonal antibody production", BIOTECHNOL BIOENG., vol. 55, no. 5, 1997, pages 783 - 92, XP002298389, DOI: doi:10.1002/(SICI)1097-0290(19970905)55:5<783::AID-BIT8>3.0.CO;2-7

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160244726A1 (en) * 2013-10-11 2016-08-25 Regeneron Pharmaceuticals, Inc. Metabolically optimized cell culture
EP3351620B1 (fr) 2013-10-11 2020-09-02 Regeneron Pharmaceuticals, Inc. Culture cellulaire à métabolisme optimisé
US11390663B2 (en) 2013-10-11 2022-07-19 Regeneron Pharmaceuticals, Inc. Metabolically optimized cell culture

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HK1223122A1 (zh) 2017-07-21
CN114717196A (zh) 2022-07-08
EA201991976A1 (ru) 2020-04-02
AU2014331776B2 (en) 2020-10-22
IL244511A0 (en) 2016-04-21
EP3055409A1 (fr) 2016-08-17
KR20230038324A (ko) 2023-03-17
JP2022009453A (ja) 2022-01-14
KR102358807B1 (ko) 2022-02-08
CA2926049C (fr) 2023-09-05
JP2016532457A (ja) 2016-10-20
AU2021200193B2 (en) 2023-08-24
KR102243980B1 (ko) 2021-04-26
CA2926049A1 (fr) 2015-04-16
AU2014331776A1 (en) 2016-03-24
HUE051049T2 (hu) 2021-01-28
HUE039551T2 (hu) 2019-01-28
ZA201601550B (en) 2023-05-31
DK3351620T3 (da) 2020-10-26
PL3055409T3 (pl) 2018-10-31
JP6663854B2 (ja) 2020-03-13
KR20220020415A (ko) 2022-02-18
MX2020011334A (es) 2021-07-30
DK3055409T3 (en) 2018-07-30
KR102610425B1 (ko) 2023-12-06
IL262833A (en) 2018-12-31
US20160244725A1 (en) 2016-08-25
ES2833471T3 (es) 2021-06-15
EP3812453A1 (fr) 2021-04-28
EP3351620B1 (fr) 2020-09-02
MX2016004564A (es) 2016-07-12
CN105637085A (zh) 2016-06-01
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AU2021200193A1 (en) 2021-03-18
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EP3351620A1 (fr) 2018-07-25
HK1253275A1 (zh) 2019-06-14
EA201690600A1 (ru) 2016-09-30
US20210087535A1 (en) 2021-03-25
EP3055409A4 (fr) 2016-09-28
JP7377243B2 (ja) 2023-11-09
SG10201800772TA (en) 2018-03-28

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